Flow distribution valve system for control of extrusion from multiple die orifices

ABSTRACT

In a thermoplastic extrusion system where a single extruder feeds molten polymer through a manifold to a plurality of separate extrusion orifices, a valve system is provided which distributes and regulates the flow of the molten polymer to the individual extrusion orifices.

CROSS-REFERENCE TO RELATED APPLICATION

This is a Continuation of copending U.S. patent application Ser. No.849,050, Nov. 7, 1977, now U.S. Pat. No. 4,170,450, and acontinuation-in-part of application Ser. No. 753,747, Dec. 23, 1976, nowU.S. Pat. No. 4,081,231.

BACKGROUND OF THE INVENTION

1. Field of the Invention

In thermoplastic extrusion operations requiring the feed of moltenpolymer from a single extruder to a pair of extrusion outlet orifices ordies, care must be taken to insure that the distribution and pressure ofthe molten polymer exiting from each die is easily regulatable withinprecise limits to insure product quality and uniformity of theindividually extruded films.

2. Description of the Prior Art

In the past, it has been common practice to feed dual tubular extrusiondies with a single extruder (not shown) as illustrated in FIG. 1. Whenit is desired to adjust the average film thickness 11 of the respectivetubes, this may be accomplished by varying the rotational speed of thepositively driven take-up nip rollers 12. An increase in nip-rollerspeed draws the still semi-molten polymer immediately adjacent theextrusion orifice away from the die 13 at a higher rate, resulting in agauge reduction of the final tubular product. Such an arrangement forgauge control adjustment can be employed only when the tubes are beingfed to separate, in-line, bag making machines due to the differential inthe rate of travel between the flattened tubes.

FIG. 2 shows an alternate prior art technique of forming two tubes froma single extruder (not shown) by extruding a relatively large tube 14,passing the extruded tube through collapsing shields 15, nip rollers 12,and subsequently slit-sealing the tube utilizing a heated wire or blade16. The forming technique has the advantage of permitting two tubularstreams to be fed through one set of wide downstream equipment, such asprinting presses and bag-making machines, but it has the drawback ofintroducing an additional heat seal seam in the finished bag productmaking such bags more susceptible to rupture under load stresses appliedduring use of the bag.

It would be possible to attain the quality advantage of the dual tubetechnique (FIG. 1) in which there is no side seal, along with theeconomic advantage of the slit-seal technique (FIG. 2) in which there isonly a single set of downstream machinery, by extruding two tubes andrunning them through the same set of nip rolls. However, this does notpermit operating the two tubes at different take-off speeds in order toadjust their relative average gauge. Such adjustment would require theemployment of a separate flow-control valve for each die.

A typical flow control valve that is commonly used in prior art is shownin FIG. 6. Molten thermoplastic material 203 is caused to flow throughgap 201, where it is subjected to a pressure drop. As the valve isadjusted by moving restrictor 202, gap 201 is changed, and the resultingpressure drop is changed accordingly. If there are two such valves inparallel, fed from a common manifold source and discharging intoidentical downstream pressures, the flow rate through the two valves isproportional to approximately the 5th power of the size of the gap.Since this gap is usually a small fraction of an inch, it may be seenthat a very small change in the size of this gap will result in anundesirably large change in flow rate. For example, if the gap is 0.1inch, and it is changed by a very small amount such as 0.005 inches,there will be a resulting change in flow through that gap ofapproximately 28 percent, provided the supply and discharge pressuresremain unchanged. Precise flow rate control with such valves is, atbest, extremely difficult. It may be seen that prior art valving meanssuch as that described above, when used in a pair (one for each die)cannot readily be used for the purpose of accurately balancing the flow,because they have the following limitations:

(a) They are not sufficiently precise to permit very accurate adjustmentof flow distribution, for the reasons described above.

(b) Adjustment of one valve results in a change in net back pressureagainst the extruder, thus causing a change in total flow leaving theextruder. Therefore, any adjustment of a valve would necessitatere-adjustment of the extruder speed in order to restore the desiredoverall average thickness of the two streams.

(c) Since there is a separate valve for each die, the operator isrequired to make a decision as to which valve to adjust. After numerousadjustments, this sometimes results in both valves being almost fullyclosed, while at another time both may be almost fully open, so there isa difference in operating conditions (back pressure) for the extruderfrom one time to another.

SUMMARY OF THE INVENTION

One embodiment of the present invention is directed to a manifold valvewhich balances the flow of molten thermoplastic resin, such aspolyethylene, between two dies which are being fed by the same extruder.The valve is located in a primary flow channel within the commonmanifold which feeds the two dies molten polymer. The molten polymer,introduced into the central portion of the manifold, is supplied from asingle, conventional, rotating screw extruder. In one embodiment thevalve comprises an elongated rod, or spool, which has a cross sectionalarea which is greater at the opposite ends of the rod than at itscentral portion. The rod, which is substantially symmetrical, has athickness at its center which at a point spaced laterally from thecenter, gradually tapers to an increased thickness section, theincreased thickness section remaining constant in cross section to theend of the rod. In another alternate embodiment of the valve structureof the present invention, the rod is constructed so that its centralportion has a greater cross-sectional area than the opposite endportions of the rod. Means are provided to impart lateral displacementto the rod, such as a captive nut which rotates on threads at one end ofthe rod. Alternatively, a fixed nut and rotatable rod may be employed.Lateral displacement of the valve rod in turn causes lateraldisplacement of its section or sections of increased cross-sectionalarea, thereby alternately increasing and decreasing the volume of theopposing end-portions of the primary flow channel. Such displacementcauses an increase in pressure drop (thus a decrease in flow) on themolten polymer flowing out one end of the manifold (i.e. the end-portionof decreased volume), while simultaneously causing a decrease inpressure drop (thus an increase in flow) on the molten polymer flowingout the opposite end of the manifold (i.e. the end-portion of increasedvolume). The resulting increase in flow at one end is equal to thedecrease in flow at the opposite end, so that the total back pressureagainst the extruder remains substantially unchanged. The total flowrate leaving the extruder is unchanged, since that flow rate isdependent on the back pressure against the extruder. Obviously theinternal cross-sectional area of the manifold flow channel must begreater than the cross-sectional area of the enlarged ends of the rod toinsure a continuous flow path of the molten polymer and permitdisplacement of the rod within the primary flow channel. Lateral rodmovement may be accomplished manually or by use of a gear motor attachedto a chain drive wheel which may be mounted on the captive nut.

In an alternate embodiment the common manifold is adapted to supplymolten polymer to three or more extrusion dies. Such adaptation isaccomplished by means of one or more secondary extrusion dies connectedto the manifold by way of secondary flow channels (one for each suchsecondary die) which intersect the primary flow channel intermediate tothe aforedescribed end-mounted dies. Each of the secondary dies isprovided with an independently controlled valve member comprising anelongated rod which is moveably mounted in the secondary flow channel tocreate a restriction of variable length therein. One end portion of theelongated rod, which is preferably tapered to minimize resistance to andturbulence in the flowing polymer stream, is inserted through the wallof the manifold and directly into the secondary flow channel between theprimary flow channel and the extrusion die orifice, thereby forming anelongated restriction therein through which the molten polymer must passprior to reaching the die orifice. In one embodiment the rod is insertedinto a substantially horizontal section of the secondary flow channelwith its tapered end portion directed into the flowing stream of moltenresins. In another embodiment the rod is inserted upwardly, into anupwardly rising portion of the secondary flow channel, and its taperedend portion is directed toward the extrusion die orifice. As with theaforedescribed spool-like valve member, means are provided on theoutside of the manifold to impart lateral displacement to the rod, suchlateral displacement directly regulating the length of the restrictioncreated by the rod. By increasing the length of this restricted portionof the secondary flow channel (and thereby decreasing the volume of thechannel), one increases the pressure drop on the molten polymer flowingtherethrough and hence decreases the rate of flow to the extrusion die.Likewise, by decreasing the length of the elongated restriction (i.e.,increasing the volume of the channel) one decreases the pressure dropand hence increases the rate of polymer flow. By appropriatemanipulation of the length of this restricted portion the extrusion rateof the molten polymer through the adjacent die orifice can be accuratelybalanced with that of the other die orifices on the same manifold.

In summary, the distribution valve apparatus of the present invention isemployed for controlling the flow of molten thermoplastic polymerstreams, such as polyethylene, in extrusion operations where it isdesired to extrude at least two such streams from a single molten resinsupply source. In one embodiment each of the molten polymer streams isfed to separate extrusion die orifices through a manifold which is fedmolten polymer from the extruder. The manifold has a substantiallycentrally located inlet for introduction of the molten polymer, andcomprises a primary flow channel which contains a flow restrictionmeans, namely the spool-type valve rod hereinabove described. The valverod is laterally displaceable in the manifold flow channel. Lateraldisplacement of the valve results in an increase in pressure drop at oneend of the manifold and an equal decrease in pressure drop at theopposite end of the manifold channel. In another embodiment additionalextrusion die orifices are attached to the single common manifold bymeans of secondary flow channels connected thereto which intersect theprimary flow channel intermediate to the two end-mounted dies. Themolten polymer flowing to each additional die is regulated by means of avalve member adjacent to the die, such valve member comprising anelongated rod inserted into the secondary flow channel, thereby creatingan elongated restriction of controllably variable length therein.

BRIEF DESCRIPTION OF THE DRAWINGS

FIGS. 1 and 2 are schematic illustrations of prior art tubular extrusiontechniques.

FIG. 3 is a schematic illustration of a portion of an extrusion systemwhich may be employed to form thermoplastic tubes utilizing theapparatus of the present invention.

FIG. 4 is a schematic illustration, in cross section, of an embodimentof the flow distribution valve apparatus of the present invention,mounted coaxially, and aligned within, the manifold flow channel.

FIG. 5 is a fragmentary view of an alternate form of flow distributionvalve in accordance with the present invention.

FIG. 6 is a typical flow control valve used in the prior art.

FIG. 7 is a front elevation, in partial cross section, of an alternateembodiment of the present invention having three tubular extrusion diesmounted on the single common manifold.

FIG. 8 is a cross-sectional top view taken along line 8--8 of FIG. 7.

FIG. 9 is a side elevation of an end-mounted extrusion die taken alongline 9--9 FIG. 7.

FIG. 10 is a side elevation of the intermediately mounted extrusion dietaken along line 10--10 of FIG. 7.

DESCRIPTION OF SPECIFIC EMBODIMENTS

In the two extrusion die embodiment of the present invention, as shownin FIG. 4, molten thermoplastic resin is supplied to manifold 21 by arotating screw type thermoplastic extruder (not shown). The moltenthermoplastic resin is passed through manifold supply channel 22 underpressure from the extruder. Manifold supply channel 22 directs thethermoplastic to primary flow channel 23, shown here as beingcylindrical in shape, where flow diverter 24 divides the entering streamto opposite ends of flow channel 23. Flow diverter 24 also acts as asupport for flow distribution valve 25 to resist the pressure of theincoming polymer without distorting valve 25. It will be noted that flowdistribution valve 25 comprises an elongated member which, in the FIG. 4embodiment, is substantially cylindrical and has a central portion ofreduced diameter, while the opposite ends of valve 25 flare out topresent cross sections having an increased diameter. The moltenthermoplastic material passes through the annulus formed by thepositioning of valve 25 in flow channel 23 and through tubular extrusiondies 26 and 27 mounted at opposite ends of manifold 21. The moltenthermoplastic material is eventually expressed in the form of tubularfilm 28 through the annular extrusion orifices (not shown) ofconventional tubular extrusion dies 26 and 27. It will be noted fromFIG. 4 that one end of the distribution valve rod 25 extends through theend of the manifold, and is threaded. The threads on the spool areengaged by threads in a nut which is restrained from lateral movement bybrackets 101. A keyway 102 in the threaded section of the spool, engagedby a key 103 fixed to a bracket 101, prevents rotation of the spoolwhile the nut may be rotated by driving motor 29 with drive chain 31 sothat lateral motion may be imparted to valve rod 25 as required.

The pressure drop of the molten polymer within the manifold supplychannel 22 will be dependent upon the size and length of the restrictionthrough which it travels before being expressed into the extrusion dies26 and 27 on opposite sides of the valve 25. The pressure drop per inchof molten polymer travel is greater in the region surrounding the largerdiameter portion of the rod 25. Accordingly, it will be seen that ifflow distribution valve rod 25 is shifted to the left, i.e., in thedirection of tubular extrusion die 26, the length of that largerdiameter portion to which the flowing thermoplastic material is exposedis reduced on the left end, and simultaneously increased on the rightend, causing a reduction in pressure drop on the left end and asimultaneous increase in pressure drop on the right end. The flow ratethrough the left end then increases until the pressure drop is the sameas it was before rod 25 was moved, and likewise the flow rate throughthe right end decreases until the original pressure drop is attained.After that has happened, the pressure in manifold supply channel 22 isthe same as it had been previously, and the increase in flow rate at theleft end has been equaled by the decrease in flow rate at the right end.

The above-described system has a particular advantage in ease ofoperation. Prior to adjusting the valve, the speed of the extruder andtake-off equipment can be established such that the average productthickness through the two dies 26 and 27 is at the desired level. Thenwhen the valve adjustment is made to produce an equal thickness fromboth dies, the average does not change. This is because the backpressure in channel 22 is not changed, therefore the pressure againstwhich the extruder must pump its output is not changed, and accordinglythe output rate from the extruder is not changed.

The above-described system has a further advantage in precision ofadjustment. If there are two such valves in parallel, fed from a commonmanifold source and discharging into identical downstream pressures, theflow rate through the two valves is inversely proportional toapproximately the cube (3rd power) of the length of the restriction.Since the initial length of that restriction is in the order of severalinches, it is possible to make a substantial change in the length toachieve a fine adjustment in flow rate. For example, if the initiallength of the restriction is 8 inches, and it is changed by asubstantial amount, such as 0.25 inches, there will be a resultingchange in flow through that gap of approximately 10 percent, providedthe supply and discharge pressures remain unchanged. This permits muchmore precise adjustment than the variable-gap prior art valve in which amovement of 0.005 inch resulted in a 28 percent change in flow rate.

The above-described system has a further advantage in that there is asingle control which may be used by the operator to re-distribute theflow. No decision is required on his part as to which knob to turn.Moving the spool to the left increases the average thickness of theproduct on the left and decreases the thickness on the right, andconversely.

The valve embodiment shown in FIG. 5 has a centrally located enlargedcross section 301 while its end portions 302 are of reduced crosssection. It will be apparent that lateral displacement of this rodcauses a displacement of the enlarged portion 301 either right or left.Such displacement causes a variation in the length of the restriction inthe end portions of the primary flow channel and results in a pressuredrop variance as described above.

An alternate embodiment of the present invention is illustrated in FIGS.7-10. Such embodiment is useful for the regulation and balancing of theextrusion rates of three or more molten polymer streams, each beingexpressed through a separate conventional extrusion die orifice mountedon a single common feed manifold. Shown in FIG. 7 is a manifold Madapted for supplying molten thermoplastic polymer (e.g., a polyolefinsuch as polyethylene) to three conventional dies (A, B & C) from acommon feed source (not shown) for the extrusion of tubular films F-1,F-2 and F-3. Dies A and C are substantially identical and are mounted onopposite end portions of manifold M. Die B, which is mounted on manifoldM intermediate to dies A and C, is substantially the same as dies A andC except that it is adapted to accommodate valve member 60, as will bemore fully described hereinafter.

Looking for the moment at FIG. 8, it is shown that the molten polymer Penters manifold M through entry port 40 and flows into primary flowchannel 41. Branching off from primary flow channel 41 are threesecondary flow channels 42, 43 and 44 which serve as conduits for thepolymer P to the dies A, B and C, respectively. The molten polymer isdistributed between secondary channels 42, 43 and 44, flows upwardlythrough dies A, B and C and is extruded from the die orifices thereof inthe form of tubular films F-1, F-2 and F-3, respectively (FIG. 7). Thefilms are thereafter drawn away from the dies in the conventional mannerand fed to the appropriate downstream processing sequences, the precisenature of which will be determined by the end-use of the film productand which are not shown.

As has been stated previously, it is highly desirable that the severalfilms each be extruded at substantially the same rate and that each beof substantially the same thickness so that optimum utilization of thesubsequent downstream equipment may be realized. These goals aresimultaneously achieved by means of the manipulation of valve members 50and 60 to controllably redistribute the flow of the molten polymer Pthrough manifold M to each of the dies A, B and C.

Valve member 50 comprises an elongated spool mounted in primary flowchannel 41 and extending through the opposing end walls of manifold M.Spool 50 is centrally positioned along the long axis of primary flowchannel 41 such that, in the embodiment illustrated, channel 41 acquiresan annular configuration along its entire length. In the embodimentshown in FIGS. 7 and 8, spool 50 is substantially symmetrical inconfiguration, having a relatively small diameter at its central portion51 which, at points spaced laterally from the center, gradually tapersto increased diameter sections 52 and 53. Sections 52 and 53 thereafterremain constant in cross-sectional area as they pass through the endwalls of manifold M and extend beyond the manifold. Bracket 54 isattached to one end of manifold M and holds moveable nut 55 such thatnut 55 is free to rotate but is restrained from significant lateralmovement. Nut 55 in turn engages the threaded end portion 56 of spool50. By rotating nut 55 spool 50 is displaced laterally, therebyrepositioning the relatively narrow section 51 within flow channel 41 inrelation to dies A and C.

The pressure drop of the molten polymer within primary flow channel 41will be dependent upon the size and length of the restriction throughwhich the polymer travels before being expressed into extrusion dies Aand C on opposite sides of the valve spool 50. The pressure drop perinch of molten polymer travel is greater in the region surrounding thelarger diameter portion of spool 50. Accordingly, it will be seen thatif flow distribution spool 50 is shifted to the left, i.e., in thedirection of tubular extrusion die A, the length of that larger diameterportion to which the flowing thermoplastic material is exposed isreduced on the left end, and simultaneously increased on the right end,causing a reduction in pressure drop on the left end, and a simultaneousincrease in pressure drop on the right end. The flow rate through theleft end then increases until the pressure drop is the same as it wasbefore spool 50 was moved, and likewise the flow rate through the rightend decreases until the original pressure drop is attained. After thathas happened, the pressure in primary flow channel 41 is substantiallythe same as it had been previously and the increase in flow rate at theleft end has been equalled by the decrease in flow rate at the rightend.

Valve member 60, which may be viewed to advantage in FIG. 10, comprisesan elongated rod 61 inserted through the wall of intermediate extrusiondie B and/or manifold M and into the secondary flow channel 43. Rod 61may be inserted into the upwardly rising section 43b of the secondaryflow channel, as shown in FIG. 10, or it may be positioned in thehorizontal section 43a thereof, in which latter embodiment the endportion of the rod will be directed into the flowing molten polymer Pentering flow channel 43. The end portion 62 of the rod is preferablytapered to minimize turbulence in the flowing stream of molten polymerand, in the case of the alternate embodiment wherein the rod is directedinto the flowing polymer, so that it will present a streamlined contourto the incoming polymer stream to minimize the resistance of the end ofthe rod to the movement of the molten fluid.

Rod 61 creates an elongated restriction in secondary flow channel 43through which the molten polymer must pass before reaching the dieorifice of extrusion die B. The rod 61 is held in fixed positionrelative to the walls of flow channel 43 but is capable of lateralmovement therein, such that the elongated restriction it creates is ofsubstantially constant and uniform cross section but is of variablelength. Valve member 60 is adjustably attached to the body of the unitby means of a bracket and rotating nut arrangement (see 64 and 65) whichengages threaded end portion 63 of rod 61 in the manner previouslydescribed with respect to bracket 54 and rotating nut 55.

A portion of the molten polymer stream P, after entering primary flowchannel 41 of manifold M, flows into secondary flow channel 43 and issubsequently expressed from the orifice of extrusion die B as tubularfilm F-2. Prior to reaching the die orifice, the molten polymer streampasses through the elongated restriction caused by valve member 60,thereby increasing the pressure drop on the stream as it passes throughchannel 43 and reducing the flow rate. By varying the length of therestriction (and thereby simultaneously changing the volume of the flowchannel) it is possible to regulate the pressure drop, and hence theflow rate, with a high degree of controllability. One is thereby able toadjust the extrusion rate of the polymer, which ultimately controls thethickness and extrusion rate of film F-2 and enables the operator tomatch film F-2 to the simultaneously extruded films F-1 and F-3.

The manner of balancing the extrusion rates and thicknesses of the threefilms is as follows. The extruder is turned on and allowed toequilibrate in the usual manner. After the films have begun beingexpressed, the extruder and downstream nip roller speeds are adjusted togive the desired average total product weight for the three webs F-1,F-2 and F-3. When this is satisfactory, the spool 50 is adjusted toachieve substantially identical product weight for the outer dies A andC. The intermediate valve member 60 is then adjusted to make the productweight from intermediate die B the same as that from the two outer diesA and C. While it is conceivable that the total extruder output maychange by a small amount when the flow rate to the intermediate die B isadjusted, any resulting change in back pressure on the extruder, andthus in extruder output, will be very small. This is because anyreduction in flow through the center die which results from anadjustment of its valve member will generally be redistributed betweenthe two outer dies, so that there will be an increase in output througheach of the outer dies that is approximately equal to half of thereduction in flow through the center die. The back pressure through oneof the outer dies is approximately proportional to the cube root of theflow, so the resulting change in back pressure on the extruder is verysmall. That is, the increase in back pressure on the extruder is aboutproportional to the cube root of the increase in flow through each ofthe outer dies, which in turn is equal to only half of the decrease inflow through the center die. As an approximate example, a 10% reductionin flow through the center die results in a 5% increase in flow througheach outer die, which then results in about 1.6% (i.e. the cube root of5%) increase in back pressure on the extruder. Consequently,readjustment of the extruder or nip speeds is, in usual practice,generally unnecessary.

The system described above has the advantage of precision of adjustment.Although the system has been described with reference to a manifoldhaving three dies mounted thereon, it will be readily apparent that sucha system may be easily expanded by providing a multiplicity ofintermediate dies patterned after the aforedescribed intermediate die B.

In any of the aforementioned embodiments, the lateral displacement ofthe adjustable valve members may be initiated and controlled in theconventional manner (i.e. by a human operator who is monitoring theaverage film thickness somewhere downstream), or by means of automaticfilm thickness detection devices which are adapted to control themovement of the valves to compensate for any differential in the gaugeof the various extruded films.

Although the present invention has been described with reference to theextrusion of tubular films of thermoplastic material, it hasapplicability to other extrusion techniques, such as the extrusion offlat films, filaments, solid tubes, foamed plastic sheets and tubes,extrusion coating, and so forth. Similarly, references in thespecification and drawings to manifolds having a single feed source areintended to be merely illustrative of the concept disclosed herein, itbeing readily apparent to those skilled in the art that a singlemanifold can be designed to handle any number of such feed sources.

It is to be understood that other modifications and variations of thepresent invention may be made without departing from the spirit andscope of this disclosure, as those skilled in the art will readilyunderstand. Such modifications and variations are to be considered ascoming within the purview and scope of the appended claims.

I claim:
 1. In an apparatus for controlling the flow of molten polymerfrom a common polymer feed source to multiple extrusion die outlets,said apparatus comprising a manifold having at least two extrusion dieoutlets thereon, a polymer inlet opening intermediate of said extrusiondie outlets and a flow channel in communication with said polymer inletand said outlets, the improvement comprising:flow restriction meansmounted axially in said flow channel, said restriction means comprisinga laterally displaceable cylindrical rod, said rod being characterizedby a narrower portion and at least one other portion of its length beingof increased diameter relative to said narrower portion, thecross-sectional area of each of the respective portions of said rodbeing substantially constant throughout the length thereof, and saidnarrower portion gradually tapering at the end thereof to said increaseddiameter portion; said portion of increased diameter forming an annularrestriction of variable length in said flow channel, each of saidrestrictions being between said polymer inlet and one of said extrusiondie outlets.
 2. In an apparatus for controlling the flow of moltenpolymer from a common polymer feed source to multiple extrusion dieoutlets, said apparatus comprising a manifold having at least threeextrusion die outlets thereon, a substantially centrally located polymerinlet opening and cylindrical flow channels between said inlet openingand each of said extrusion die outlets, the improvement comprising:flowrestriction means mounted axially in each of said flow channels, saidrestriction means comprising a laterally displaceable elongatedcylindrical rod, said rod forming an annular restriction of variablelength and substantially uniform cross-section in said flow channel,each of said restrictions being between said polymer inlet and one ofsaid extrusion die outlets, and the portion of said rod forming themoveable end of said annular restriction being tapered to minimizeturbulence in the polymer flowing through said flow channel.